Cyclic adsorption processes for removal and/or recovery of condensable hydrocarbons from natural gas



Feb. 18, 1958 E. B. MILLER 2, oycmc ADSORFTION PROCESSES FOR REMOVALAND/OR RECOVERY OF CONDENSABLE HYDROCARBONS FROM NATURAL GAS Filed Feb.8, 1957 6 Sheets-Sheet 1 INVENTOR. 521M557 5. MHZ/f2 BY, +M

2,823,764 ND/OR RECOVERY OF CONDENSABLE HYDROCARBONS FROM NAT Filed Feb.8, 1957 Feb. 18, 1958 E. B. MILLER CYCLIC ADSORPTION PROCESSES FORREMOVAL A mam. GAS

6 Sheets-Sheet 2 INVENTOR [RA E57" B mum ATTORNEYS Feb. 18, 1958 E. B.MILLER 2, ,7

CYCLIC ADSQRPTION PROCESSES FOR REMOVAL AND/QR RECOVERY OF CONDENSABLEHYDROCARBONS FROM NATURAL GAS Filed Feb, e. 1957 e SheetEs-Sheet s Fl6..4. f} #0 INVENTOR ATTORNEYS Feb. 18, 1958 E. B. MILLER 2,323,764

cycuc ADSORPTION PROCESSES FOR REMOVAL AND/OR RECOVERY OF CONDENSABLEHYDROCARBONS FROM NATURAL GAS Filed Feb. 8, 1957 6 Sheets-Sheet 4 F I e.5. O a

O o O O O 6 J/ O O O D O a o o o 2/ o o 6, O

o w o o O O o O O o O 0 o O o O INVENTOR" ERNEST B. mum

ATTORNEYS Feb. 18, 1958 E. B. MILLER 2,823,764

CYCLIC ADSORPT O PROCESSES FOR REMOVAL AND/OR R C VERY OF ,CONDEN LEHYDROCARBONS FROM NAT L G Filed Feb. 8, 1957 Sheets-Sheet 5 Fl G.9

INVENTOR ERNEST-RHILLER 4&4?

ATTORNEYS Feb. 18, 1958 E. B. MILLER 2,323,764

CYCLIC ABSORPTION PROCESSES FOR REMOVAL AND/OR RECOVERY OF CONDENSABLEHYDROCARBONS FROM NATURAL GAS Filed Feb. 8, 1957 6 Sheets-Sheet 6 FIG.ll;

FIG. IO.

INVEN'I OR ER NEST 8. M1 LL ER BY ,L W

ATTORNEYS United States Patent CYCLIC ABSORPTION PROCESSES FOR REMOVALAND/ OR RECOVERY OF CONDENSABLE HY- DROCARBONS FROM NATURAL GAS ErnestB. Miller, Houston, Tex., assignor to Jefferson Lake Sulphur Company,New Orleans, La., a corporation of New Jersey Application February 8,1957, Serial No. 639,006

4 Claims. (Cl. 183-114.2)

This invention relates to gas dehydrating and has more particularreference to a continuous process for removing moisture and condensablehydrocarbons from wet natural gas at the source, prior to thetransmission thereof through pipe lines, and recovering the condensablehydrocarbons.

One object of the present invention is to provide a novel and improvedcyclic adsorption process for dehydrating wet natural gas of the typecomprising an adsorption cycle in which the natural gas being treatedpasses through one or more adsorption stages of the adsorber; and anactivation cycleemploying a captive activation gas recycled through aheater, the activation stage of the adsorber, and a condenser separator.

Another object of the present invention is to provide a novel andimproved cyclic adsorption process for the removal and/or recovery ofwater vapor and condensable hydrocarbons from wet natural gas, ascharacterized above, including two activation cycles to effect a morecomplete activation and a more complete removal of the products to berecovered, and three purging cycles, a first purging cycle precedingthe-first activation cycle, a second purging cycle intermediate the twoactivation cycles, and a third purging cycle following the secondactivation cycle to prevent dilution of the activation gases by slippagegas and also prevent the loss of desorbed products by slippage of theactivation gas into the outgoing efiluent stripped natural gas, and acondenser separator through which the recycling captive activation gasused in the first 6C." tivation cycle passes, to remove the water vaporand condensable hydrocarbons. therefrom.

A further object of the present invention is toprovide a novel andimproved cyclic adsorption .processfor the removal and/or recoveryofwater vapor and. condensable hydrocarbons from wet natural gas, ascharacterized above, wherein the captive activation gas employed in thesecond activation stage has a lower hydrocarbon content and is heated toa higher temperature than the captive activation gas employed in thefirst activation stage so as to efiect a very complete removal of thedesired hydrocarbons.

Other objects and advantagesof the invention will appear in thefollowing specification when considered in connection with theaccompanyingdrawings, in which:

Fig. 1 is a schematic view showing one embodiment of apparatus and thearrangement thereof for carrying out the method of the present inventionand the flow of the various fiuids therethrough;

Fig. 2 is a side elevational view of the adsorber shown in Fig. 1;

Fig. 3 is a plan view of theapparatus shown in Fig. 2;

Fig. 4 is a vertical sectional view taken onthe line .4--4 of Fig. 3,but. omitting the driving apparatus;

Fig. 5 is a horizontal sectional view taken ,on the line 5--5 of Fig. 4;

Fig. 6 is a fragmentary sectional view taken .ona the line 66 0f Fig.4,-showing themanner of bracing the upper ends of the elongated adsorbentmaterial containing vessels;

Fig. 7 is a fragmentary sectional view taken on the line 7.7 of Fig. 4,showing the manner of supporting the lower ends of the elongatedadsorbent material containing vessels;

Fig. 8 is a horizontal sectional view takenon the line 8-8 of Fig. 4;

Fig. 9 is a detailsectional view, taken on the line 99 of. Fig. 8;

Fig. 10 is a vertical sectional view, with parts broken away, oftheadsorbent material containing vessels shown in Fig. 4, showing thecontainers for holding the adsorbent material mounted therein; and

Fig. 11 is a plan view of the container shown in Fig. 10. The presentinvention is drawn to a novel method of dehydrating wet natural gasunder high pressure and removing the condensable hydrocarbons therefrom,and is an improvement over the method disclosed and claimed in myco-pending application Ser. No. 623,862, filed November 23, 1956, forCyclic Adsorption Process.

The present invention provides a novel and improved process for removingand/ or recovering water vapor and condensable hydrocarbons from wetnatural gas. The process is a continuous cyclic adsorption processemploying an adsorber in. which at least one bed of adsorbed material ismaintained in a plurality of stages and, in general, comprises anadsorption cycle in which a continuous flow of the natural gas beingtreated is directed, under high pressure, through one or more adsorptionstages so that the contained water vapor .and condensable hydrocarbonswill be adsorbed by the beds of adsorption material therein; a firstactivation cycle in which a flow of a captive activation medium, underhigh pressure, is continuously recirculated through a heater and a firstactivation stage to vaporize the moisture and condensable hydrocarbonscontained in the adsorbent material therein and reactivate the adsorbentmaterial; a second activation cycle in which a flow of a captiveactivation medium, under high pressure, is continuously recirculatedthrough a heater and a second activation stage to vaporize the moistureand condensable hydrocarbons contained in the adsorbent material thereinand reactivate the adsorbent material; a first purging cycle in which aportion of the recycling activation medium used in the first activationcycle is continuously diverted and passed into a stage immediatelypreceding the first activation stage, called the first purging stage,with the efiiuent gas from the first purging stage passing into the flowof the gas being treated on its way to the first adsorption stage; asecond purging cycle in which a portion of the recycling activationmedium used in the second activation cycle is continuously diverted andpassed into a stage, intermediate the first activation stage and thesecond activation stage, called the second purging stage, with theefliuent gas from the second purging stage passing into the flow of thecaptive activation medium being recycled through the first activationstage; a third purging cycle in which a portion of the efiluent strippedgas being treated from the last adsorption stage is continuouslydiverted and passed into a stage immediately following the secondactivation stage, called the third purging stage, with the effluent gasfrom the third purging stage passing into the flow of the captiveactivation medium being recycled through the second activation stage;the periodical shifting of the relative positions of the particularadsorbent material and the particular flow of fluid through each stage,either by moving the beds of ad sorbent material through the stages orby shifting the flows of fluid through the several stages, so that eachstage becomes, in succession, a first purging stage, a first activationstage, a second purging stage, a second activation stage, a thirdpurging stage, and an adsorption stage; and a product recovery cycle inwhich the fiow of the recycling activation medium used in the firstactivation stage, after its passage through the first activation stage,passes through a condensing and separating zone where the water vaporand condensable hydrocarbons are condensed and recovered with thestripped activation gas from the condensing and separating zone passingback into its recycling path.

While any suitable usual type of adsorption apparatus may be employed topractice the process of the present invention, for purpose ofillustration, the process will be described as carried out by employinga rotary type of adsorber in which a plurality of elongated uprightclosed vessels containing adsorbent material are rotated directly insuccession and substantially continuously through the various stages ofthe adsorber;

Referring now to the drawings, there is shown, in Fig. 1, one embodimentof apparatus and arrangement thereof for carrying out the process of thepresent invention. The apparatus shown includes a seven stage rotaryadsorber 1. two stages of which are employed as adsorption stages. twostages of which are employed as activation stages, and three stages ofwhich are employed as purging stages; a pair of heaters 2, 2' forheating the activation gas used in the two activation stages; a pair offans or blowers 3, 3' for recirculating the activation gases through theactivation stages; and a condenser-separator 4 employed to condense themoisture and condensable hydrocarbons contained in the recirculatingactivation gas in the first activation stage after the gas has passedthrough the first activation stage of the adsorber.

The wet gas being treated is delivered, at high pressure, from theususal compressor or source of supply (not shown) to the firstadsorption stage of the adsorber by means of a pipe line 5. The gaspasses through the first adsorption stage, where some of the moistureand condensable hydrocarbons are removed. From the first adsorptionstage of the adsorber, the gas passes through pipe line 6 to the secondadsorption stage of the adsorber. An intercooler may be employed to coolthe gas before it passes into the second adsorption stage of theadsorber, if desirable. After passing through the second adsorptionstage, the moisture and condensable hydrocarbon stripped gas passesthrough pipe line 7 to its various points of use.

The captive activation gas for the first activation stage is heated inthe heater 2 to a temperature of about 400 F., and from the heater,passes through a pipe line 8 to the first activation stage of theadsorber. The heated gas passes upwardly through the first activationstage, desorbing the accumulated moisture and hydrocarbons from theadsorbent material therein. The heated gas and the moisture vapor andcondensable hydrocarbons desorbed from the adsorbent material passthrough a pipe line 9 to the condenser-separator 4, where the moisturevapor and condensable hydrocarbons are condensed and separated. Thewater and hydrocarbons are drained from the bottom of the separator bymeans of a suitable drain pipe. From the condenser-separator 4, the nowstripped activation gas passes through a pipe line 10 to the blower orfan 3 and is recirculated by the blower through a pipe line 11 and theheater 2 back through the first activation stage of the adsorber. Thisrecirculation process is continuous. I

The captive stream of gas in the first activation cycle is circulated,by means of the blower 3, through the heater 2, the first activationstage of the adsorber and the condenser-separator 4. The composition ofthis stream will. build up gradually in terms of condensable vapors,composed chiefly of hydrocarbons, until the dew point of the captive gasstream reaches condenser temperature and will, thereafter, yield asliquid all the con.- densable vapors desorbed in the first activationstage of the adsorber.

The captive activation gas for'the second activation stage is heated inthe heater 2' to a temperature of about 500 F., and from the heater,passes through a pipe line 12 to the second activation stage of theadsorber. The heated gas passes upwardly through the second activationstage desorbing the accumulated moisture and hydrocarbons from theadsorbent material therein. The heated gas and the moisture vapor andcondensable hydrocarbons desorbed from the adsorbent material passthrough a pipe line 13 to the blower 3 and are recirculated by theblower through a pipe line 14 and the heater 2' back through the secondactivation stage of the adsorber. This re,- circulation process iscontinuous.

The vessels which contain the adsorbent beds are rotated so that eachvessel passes in succession through the various stages of the adsorber.As the vessels 'move through each stage they are filled'with theparticular gas flowing through the stage and carry this gas into thenext or succeeding stage in their rotary movement. This carrying of gasfrom one stage to the other by the vessels is called slippage.

In order to prevent slippage gas from the first adsorption stage, whichwould consist of the raw gas being treated, from being carried over intothe first activation stage and diluting the recycling activation gas, apurging stage is interposed between the first adsorption stage and thefirst activation stage and called the first purging stage.

In order to prevent slippage gas from the first activation stage, whichis very richlin condensable hydrocarbons, from being carried over intothe second activation stage, a purging stage is interposed between thefirst activation stage and the second activation stage, called thesecond purging stage.

Also, in order to prevent the slippage gas from the second activationstage, which contains some condensable hydrocarbons, from being carriedover into the second adsorption stage, where 'it would pass out of theadsorber with the outgoing stripped natural gas, a purging stage isinterposed between the second activation stage and'the second adsorptionstage, called the third purging stage.

A portion of the captive activation gas employed in the first activationcycle flowing to the heater 2 through pipe line 11 is continuouslydiverted through pipe line 15 for use as thepurging gas in the firstpurging stage. The effiuent gas from the first purging stage passesthrough pipe line 15' back into pipe line 5 to join the flow of the rawgas being treated on its way to the first adsorption stage of theadsorber. This permits the purging gas in the first purging stage topush the slippage gas in the first purgingstage, which consists of rawgas, back into the incoming raw gas being treated on its way to theadsorber. And, as the gas used as the purging gas in the first purgingstage consists of diverted activation gas from the first activationstage, the slippage gas from the first purgingstage into the firstactivationstage would consist of activation gas, so that the recyclingactivation gas would not be diluted.

A portion of the captive activation gas employed in the secondactivation cycle flowing to the heater 2 through pipe line 14 iscontinuously diverted through pipe line 16 for use as the purging gas inthe second purg ing stage. The efiiuent gas from the second purgingstage passes through pipeline 17-into pipe line 10 and joins therecycling activation gas used in the first activation cycle. Thispermits the purging gas in the second purging stage to push the slippagegas in the second purging stage, which consists of activation gas fromthe first activation stage, back into the recycling stream of theactivation gas used in the first stage. And, as the gas used as thepurging gas in the second purging stage consists of diverted activationgas from the second activation stage, the slippage gas from the secondpurging stage into the second activation stage would consist ofactivation gas so that the recycling activation gas in the secondactivation stage wouldnot be diluted. .L i j .A portion of the eflluentstripped gas flowing fromthe second adsorption stage of the adsorberthrough pipe line 7, is continuously diverted through pipe line 18 foruse as the purging gas in the third purging stage. The efiiuent gas fromthe third purging stage passes through pipe line 19 into pipe line 13and joins the recycling activation gas used in the second activationcycle. This permits the purging gas in the third purging stage to pushthe slippage gas in the third purging stage, which consists ofactivation gas from the second activation stage and containshydrocarbons, back into therecycling stream of the activation gas usedinthe second activation stage. And, as the gas used as. the purging gasin thethirdpurging stage consists .of diverted efliuent stripped naturalgas from the secondadsorption stage,.the slippage gasfrom the thirdpurging stage intothe second adsorption stage would consist of strippednatural gas so that no condensable hydrocarbons would belost.

The employment of the two activation cycles and the three purgingcycles, as above outlined, effects a very complete removal of thedesired hydrocarbons and increases the efficiency and operation of theadsorber.

While any suitable type of rotary adsorber may be employed to practicethe method of the present invention, the adsorber illustrated isgenerally similar to the fluid treating apparatus shown in my Patent No.2,751,033 issued June 19, 1956, for Fluid Treating Apparatus.

As shown in Figs. 2 to 11, inclusive, the adsorber comprises anelongated upright cylindrical pressure vessel 20 having flangedvertically aligned circular openings 21, 22 in its top and bottom walls,respectively, closed by top and bottom flanged cover plates 23, 24removably secured to cover said openings, as by bolting; suitableframework, indicated at 25, for supporting the vessel 20 in an uprightposition, a rotatable vertical shaft 26 extending through the pressurevessel 20 with its upper end journaled in a suitable cap bearing carriedby the upper closure member 23 and with its lower end extending througha suitable shaft seal, secured to the bottom of the lower closure member24; a vertical shaft 27 coupled to the bottom end of the shaft 26 andconnected to suit able differential gearing, indicated at 28, driven bya motor 29; a support disc 30 fixedly mounted on the shaft 26 forrotation therewith within said pressure vessel and providing support fora plurality of elongated fluid treating material containing cylindricalvessels 31; upper and lower distributive assemblages, indicatedgenerally at 32, 33, each assemblage comprising an annular stationarymember 34 having a plurality of compartments or manifolds formedtherein, a tube sheet disc valve 35 slidably mounted on the shaft 26 forrotation therewith, a spring support disc 36 fixedly mounted on theshaft 26 and supporting a plurality of coiled springs 37 which engagethe tube sheet disc valve 35 and tightly press it against the open endof the annular stationary member 34; a plurality of flexible pipes 38,each connecting the upper end portion of one of the vessels 31 and thetube sheet disc valve 35 of the upper distributive assemblage; aplurality of flexible pipes 39, each connecting the lower end por-. tionof one of the vessels 31 and the tube sheet disc valve 35 of the lowerdistributive assemblage, a plurality of inlet-outlet conduits, sevensuch being shown, 40, 41, 42, 43, 44, 45 and 46, connected to theannular stationary member 34 of the upper distributive assemblage andextending upwardly through the upper cap closure member 23, for theingress and egress of fluids to and from the upper stationary member 34;and a plurality of inletoutlet conduits, seven such being shown, 40',41, 42', 43, 44', 45 and 46, connected to the annular stationary member34 of the lower distributive assemblage and extending downwardly throughthe lower cap closure member 24 for the ingress and egress of fluids toand from the lower stationary member 34. The cylindrical pressure vessel20 and the cap cover members 23, 24 arepreferably made of heavyboilerplate. The flanges formed on the peripheries of the openingsMZl, not thevessel 20 andthe peripheries of the capcover members 23, 24 arepreferably formed of heavy iron rings, rectangular in cross section andare welded to the peripheral edges of the openings and the cover plates,asindicated at 47.

The shafting 26, preferably and as shown, is formed of three sections,an upper section 48, an intermediate section 49, and a lower or bottomsection 50. The upper andlower sections 48 and 50 consist of solid rod,round in cross section. The intermediate section 49 consists of a hollowpipe having an internaldiameter considerably larger than the diametersof the upper and lower sections.

The .upper section 48 has its upper end journaled in a suitable capbearing 51 carried by the upper cover member 23 and its lower endsupported in a support bushing 52 mounted in the upper end of theintermediate section 49 with a pin 53 passing through the two sectionsand the bushing for rigidly and detachably securing the two sectionstogether.

The bottom section 50 has its upper end engaged in a support bushing 54mounted in the lower end of the intermediate section 49 with a pin 55passing through the two sections and the bushing for rigidly anddetachably securing the two sections together, and with its lower endextending through the lower cover member 24 and a suitable shaft seal 56and coupled to the upper end of the shaft 27.

The support disc 30 which supports the cylindrical vessels 31 iscomposed of two semi-annular fiat pieces 57, the inner adjacent straightedges of which are provided with flanges which are bolted together toform the complete disc. This is to permit of assembling the disc withinthe pressure vessel 20.

The disc 30 (see Figs. 4 and 7) is fixedly secured, as by bolting, to acollar 58 fixedly secured to the intermediate section 49 of the shaft26, so that the disc will rotate with the shaft. The outer peripheraledge portion of the disc 30 is supported by means of a plurality ofsupporting links or arms 59, each having its upper end bolted to one ofa plurality of circumferentially spaced lugs 60 carried by a collar 61fixedly secured to the intermediate section 49 of the shaft 26 and itslower end bolted to one of a plurality of circumferentially spacedupstanding lugs 62 secured to the upper surface of the disc 30.

The vessels 31 are supported by the disc 30, as by means of a pluralityof supporting links or arms 63 in the form of short sections ofstructural angles, each arm 63 having its outer end portion fixedlysecured to the bottom and one side of one of said vessels 31, as bywelding, and its inner end portion fixedly secured, as by bolting, toone of a plurality of circumferentially spaced dependent lugs 64, in theform of short sections of I-beams, welded to the under surface of thedisc 30 (see Figs. 4 and 7).

Means may be provided for holding the cylindrical vessels 31 in theirupright position encircling the shaft 26. In the particular embodimentof the invention illustrated, such means are shown as comprising a disc65 composed of two semi-annular fiat pieces 66, 66, the inner adjacentstraight edges of which are provided with flanges which are boltedtogether to form the complete disc. This is to permit of assembling thedisc within the pressure vessel 20. The disc 65 (see Figs. 4 and 6) isfixedly secured, as by bolting, to a collar 67 fixedly secured to theintermediate section 49 of the shaft 26, so that the disc will rotatewith the shaft. The upper end portions of the vessels 31 are held intheir upright position by the disc 65, as by means of a plurality ofbracing strips or arms 68 in the form of short sections of structuralangles. Each arm 68 has its outer end bolted to a lug 69 welded on theouter surface of one of the vessels 31 and its inner end portion fixedlysecured, as by bolting, to the upper surface of the disc 65.

The upper and lower distributive assemblages 32, 33 are identical inconstruction and, as shown in Fig. 4, each comprises an annulartrough-shaped stationary member 34 having a plurality of compartments ormanifolds formed therein; a tube sheet disc .valve 35 slidably mountedon the shaft 26 for rotation therewith; and a spring support disc 36fixedly mounted on the shaft 26 and supporting a plurality of coiledsprings 37 which engage the tube sheet disc valve 35 and tightly pressit against the open end ofv the annular stationary member 34.

The upper and lower annular stationary members 34 are, identical inconstruction and, as shown in Figs. 4, 5, 8 and 9, each is formed in theshape of an annular trough having an annular top (or bottom) wall 70 andannular side walls 71, 72 (see Figs. 4 and 9). 1

The member 34 is divided into a plurality of compartments or manifolds,as by means of a plurality of circumferentially spaced pairs of wallmembers 73 extending transversely of the member 34 and having'their top(or bottom) and side walls welded to the top bottom) and side walls ofthe member 34 to form gas-tight joints. Seven such compartments ormanifolds are shown and, for the purposes of clarity of description,designated manifolds a," b, c, d, e, and g," respectively. See Fig. 8.

Theupper member 34 of the upper distributive assemblage '32 is heldstationary relative to the rotation of the shaft 26 and the upper tubesheet disc valve 35 by the upper inlet-outlet conduits 40, 41, 42, 43,44, 45, and 46, which are welded to the upper cap closure member 23 andhave their lower ends Connected, as by welding, to the manifolds a, b,c, d," e, "f and g, respectively, in the upper member 34 to providecommunication therewith.

The lower member 34 of the lower distributive assemblage is heldstationary relative to the rotation of the shaft 26 and the lower tubesheet disc valve 35 by the lower inlet-outlet conduits 40', 41', 42, 43,44', 45, and 46, which are welded to the lower cap closure 24'and havetheir upper ends connected, as by welding, to the manifolds a, b, c, d,e, f and g," respectively, in the lower member 34 to providecommunication therewith.

The upper and lower tube sheet disc valves 35 are identical inconstruction and, as shown in Fig. 4, each comprises a flat metal dischaving a plurality of circumferentially spaced circular openings 74formed in a circular row adjacent its periphery. The disc is providedwith a collar 75 having a plurality of radially extending reinforcingribs welded to its bottom surface or cast integral therewith. The collar75 is keyed on the upper (lower) section of the shaft 26 to havelongitudinal movement therealong as well as rotative movement therewith,as by means of a set screw 76 slidably engaging in a longitudinal groove77 formed in the upper (lower) section of the shaft 26. A second collar78 is fixedly secured to the shaft 26 immediately beneath the collar 75to limit the inward movement of the disc as it moves longitudinally ofthe shaft 26. The disc 35, as well as the collar 75, are loosely fittedon the shaft 26 so that the disc valve can be moved slightly to conformto any change in the plane of the engaged surface of the stationarymember 34, due to unequal expansion and contraction.

The tube sheet disc 35 is so mounted on the shaft 26 that it slidablyengages the open bottom (top) end of the annular stationary member 34with the circular row of openings 74 vertically aligned with themanifolds a, [2," c," d, e, "f and g, so that each manifold will be incommunication with a group of the circular openings.

The upper and lower spring support discs 36 are identical inconstruction and, as shown in Fig. 4, each comprises a metal discmounted on the shaft and having a hub 79 provided with a plurality ofcircumferentially spaced radial ribs or webs welded to the under face ofthe disc to strengthen it. The hub is fixedly secured to the shaft, asby a set screw. Aplurality of vertically extending circumferentiallyspaced coiled springs 37 are interposed between the tube sheetdisc valve35 and thespring sup-= port disc 36. In order to insure that the springs37 remain in proper. position, they are mounted on and between shortstubs 80 extending upwardly from the disc 36 and short correspondingstubs 80 extending downwardly from the disc 35. The construction andarrangement is such that the springs 37 will keep the disc valve 35evenly and firmly pressed into engagement with the under surface of theannular stationary member 34.

The upper and lower flexible pipes 38, 39, which connect the upper andlower end portions of the adsorbent material containing vessels 31 tothe upper and lower distributive assemblages are identical inconstruction and, as shown in Figs. 4 and 10, each comprises a thinwalled cylindrical metal tube having the greater portion of its wallformed in a sinuous shape to give it flexibility, the outer cylindricalend of each tube is'detachably secured to a nozzle 81 formed on theupper (lower) end portion of the vessel 31, as by strapping. Thecylindrical inner end of the tube is provided with an integral flange82. The opening in the cylindrical inner end of the tube is aligned withone of the circular openings 74 formed in the upper (lower) tube sheetdisc valve 35 and the flange 82 is detachably secured to the outersurface of the disc valve, as by countersunk bolts, so that the innersurface of the disc wall will be smooth and uninterrupted (see Fig. 4.)

To prevent the escape of gas between the rotating tube sheet disc valve35 and the manifolds in the member 34, sealing ring gaskets 83 areplaced at the juncture of the side walls of the member 34 and the discvalve 35. The ring gaskets 83 are wedged into annular troughs 84,secured, as by welding, to the outer surface of the side walls of themember 34. Each trough comprises an annular top (bottom) wall 85 and anannular side wall 86. The ring gaskets 83, preferably and as shown,comprise a plurality of annular strips of packing, generally rectanagular in cross section and made of any suitable material, such as Teflonor impreganated asbestos.

The seven manifolds a, b, c, d, e, f, and Hg" are sealed off from eachother by means of cross seals 87, each sealed into a recess 88 formed bythe adjacent end walls of the manifolds and a bottom plate 89 verticallyspaced from the open end of the manifolds (see Figs. 8 and 9). Eachcross seal is tightly wedged in its recess with its outer ends in tightengagement with the adjacent side walls of the annular seals 83 and withits bottom surface in sealing engagement with the upper (lower) surfaceof the tube sheet disc. In order for the outer ends of the cross sealsto engage the adjacent side walls of the annular seals 83, the portionsof the side walls 71 and 72 of the member 34 which extend between eachpair of adjacent transverse members 73 are cut away, as indicated at 90,for a distance equal to the thickness of the seals 83 (see Fig. 9). p

The widthsof the manifolds a, b, c, d, e, "f? and g are substantiallythe same as the internal diam eters of the circular openings 74 in thetube sheet disc 35, so that each cross seal can effectively seal off oneof the openings.

Each of the openings 74 formed in the upper tube sheet disc 35, is invertical alignment with a corresponding one of the openings 74 formed inthe lower tube sheet disc 35 and eachof the cross seals 87 whichseparate the manifolds a, b, c, d, e, f and g formed in the upperstationary member 34 is in vertical alignment with a corresponding oneof the cross seals 87 which sepa+ rate the manifolds a, b, c, d, e, inand git formed in the lower stationary member 34.

When the rotary disc valves 35 and the vessels 31 are stationary, theforegoing arrangement, in effect, divides the adsorbent materialcontaining vessels 31 into seven groups, with one group connected tocommunicate with the mani folds a, one group connected to communicatewith the manifolds b, one group connected to communicate with themanifolds c, one group connected to communicate '9 with the manifolds"d, one group connected to communicate with the manifolds e, one groupconnected tocommunicate with the manifolds f, and one groupconnected tocommunicate with the manifolds g. Each group of vessels 31, togetherwith the upper and lower manifolds with which they ate in communicationform separate flow passages through the adsorber so that seven separate,distinct and continuous flows of fluid may pass through the apparatus.Each flow entering the upper distributive assemblage by means of one ofthe inlet-outlet conduits 40, 41, 42, 43, 44-, 45 or 46, thence throughone of the groups of vessels 31 into the lower distributive as-'semblage and out through one of the inlet-outlet conduits 40', 41, 42,43', 44, 45', or 46'. As the vessels 31 and the upper and lower discvalves 35 rotate, each of the flows of fluid will successively passthrough the vessels 31. For convenience in description, each flowpassage is called a stage, in which either adsorption, activation, orpurging takes place, dependingupon the particular fluid flowingtherethrough. Also, the vessels 31 are called zones, in which eitheradsorption, activation or purging takes place, depending upon theparticular fluid flowing therethrough at a given time.

The silicagel containing vessels 31 are identical in construction and,as shown in Figs. and 11, each comprises an elongated hollow tubularmember 91 having a closed bottom end and an open upper end provided witha'flanged collar 92 to which is secured, as by bolting, a removablecover plate 93.

A horizontally disposed annular disc 94 is mounted in the lower endportion of the member 91 and secured therein, as by :welding, to form agas-tight joint between the outer peripheral edge of the disc and theside wall of the member 91. The lower annular disc 94 forms a sup portfor an elongated annular fluid treating material container 95. Thecontainer 95 is removably mounted within the member 91, withitsbottomend resting on the annular disc 94 and with the longitudinalopen end of the eon tainer aligned with the opening in the disc.

The tubular member 91 has a tapered side wall for a purposehereinafterto be described and is providedwith upper and lower circular openings96in which are secured, asby welding, the nozzles 81 to which the upperand lower flexible pipes 38and 39 are secured.

A baffle member 97 ismounted in the space between-the bottom of themember 91 and the annular disc 94, and

an upper baflle member 98 is secured to the underside of the cover plate93 and is removable therewith. The upper and lower baflle members 98 and97 are identical in construction and, as shown in Fig. 10, eachcomprisesa generally elliptical-shaped flat sheet 99 extending upwardly(downwardly) from the bottom (top) of the member 91 to insure an'evenflow of fluid through the member 91; a side wall forming member 100; andinsulating material 101 placed within the pocket formed by the members99 and 100 and the bottom (top) wall of the member 91 (see Fig. 10).

The-containers 95 are identical in construction and, as shown in Figs.10 and 11, each comprises two concentric tubular screens 102, 103, heldin spaced-apart relation by a plurality of longitudinal radial fins 104,with the annular space between the screens closed at the bottom, as by aflanged annular plate 105. The mesh of the screens is such as to retaina granular adsorbent material 106 in the annular space between thescreens. In the instant case,

the adsorbent material may be of any adsorbent having characteristicssubstantially like silica gel or the gel of other activated hydrousoxides. used.

Each of the containers 95 is closed at its top by means of concentrichoops or metal bands 107, 108 mounted on Preferably silica gel is theconcentric screens 102, 103, and a cover plate 109 is detachablyconnected to the inner hoop or band 108, as

by screws, and having a depending annular flange 110 fitting between thehoops or bands 107, 108. A depending,

i0 cylindrical fin 111 is secured to the-flange 'and pro jectsdownwardly'between and below the hoops or bands 107, 108, and fits inslits 112 formed in the upper ends of the radial fins 104, all as shownin Figs. 10 and 11. The construction is such that, as the silica gelsettles down, leaving a space between the top portions of the wirescreens devoid ofsilica gel, the fin 111 will. prevent fluid frompassing through the space.

Mounted within the inner wire screen 103 is an invertedsubstantiallyconically shaped baflie member 113. The baflle member 113is closed at its apex which extends downwardly to a point near thebottom of the container and has its upper peripheral edge-suitablysecured to the band 108, as by welding. Preferably, the baflle member113 is made of thin sheet metal.

When the container 95 is mounted within the hollow member 91, as shownin Fig. 10, the elongated annular space 'between the walls of the member91 and the inverted conical baflie'member 113 forms an elongatedfrusto'conically shaped duct which is-annular in cross section. Theannular container, filled with silica gel, is positioned in theductbetween the members 91 and 113 in such manner that it forms abarrier extending longitudinally across the duct from top-to bottom. Thecross sectional areasof the duct at its top'and bottom are substantiallyequal and the tapers of its side walls are such that a substantiallyuniform velocity is obtained on both sides of the barrier as fluid istransferred from the upstream to the downstream side, regardless of thedirection of flow, thereby creating a substantially constant static headover theface of the barrier, resulting-in a substantially uniformdistribution of the fluid throughout the entire barrier area. Thus, itwill be-seen that by using the members 91 and 113, as baflle members,the entire area is made use of with resultant increase in efficiency,capacity and economy.

Means-may be provided so that-the containers 95 which hold the adsorbentmaterial may readily be removed from and replaced in the=vessels 31. Asshown, such means may comprise an opening 114 formed in the top of thevessel20having a cylindrical member 115 welded therein and provided witha readily removable closure disc 116 secured in-the'upper end ofthe'member- 115," as by means of a split shear ring117bolted thereto andfitted into a circumferential recess 118 formed in the inner surface ofthemember 115, and an O-ring packing 119 mounted between the closuredise116*and theside wall of the member 115 to insure gas tightness.

T he flows of the various gases through the various stages of theadsorber and the auxiliary apparatus are manifold a the gas passesthrough openings 74 formed in the upper tube sheet disc valve 35 andflexible pipes 38 into the upper endportion of the group of vessels 31..which'areat that time in communication with the maul-- The gas'passesdown through the silica gel fold a. beds therein into the bottoms ofthe-vessels. The baffle members 113, in cooperation with the taperedside walls of the vessels 31, insure a substantially uniform flow and.

distribution of the gas through the silica gel beds, which adsorb someof the water vapor and condensable hydrocarbonsfromthe gas. From thebottoms of the vessels 31, the now partially dried gas passes throughoutlet pipes 39 andopenings 74 in the lower tube sheet disc valve 35,

into the manifold a of the lower distributive assemblage. Fromthelowermanifold a of the lower distributive assemblage, the gas passes throughinlet-outlet conduit 40 and pipe line 6 to the second adsorption stageand enters;manifold-b of the lower distributive assemblagef throughinlet-outlet conduit 41. From the lower man}, told b the gas passesthrough openings 74 in the tube sheet'disc valve 35 and inlet pipes 39into the lower end portion of the group of vessels 31 which are at thattime in communication with manifold b. The gas passes upwardly throughthe vessels 31 of the second group and through the silica gel bedstherein into the tops thereof, additional water vapor and condensablehydrocarbons being adsorbed from the gas during its passage through thesilica gel beds.

From the tops of the vessels 31 of the second adsorption group, the gaspasses through pipes 38 and openings 74 in the upper tube sheet discvalve of the upper distributive assemblage into the upper manifold b.

From the upper manifold b the gas passes through inlet-outlet pipe 41and pipe line 7 to the various points of use.

The removal and recovery of the moisture and hydrocarbons from the bedsof adsorbent material is effected in the first activation stage. Theactivation gas, a captive gas, is heated in a heater 2, where itstemperature is raised to about 400 F., depending upon the moisturecontent and the type of hydrocarbons to be recovered. From the heater,the heated activation gas passes through pipe line 8 and inlet-outletconduit 45 into the lower manifold of the lower distributive assemblage.From the manifold f the hot activation gas passes through openings 74 inthe lower tube sheet disc valve 35 and flexible pipes 39 into the lowerend portions of the groups of vessels 31 which are at that time incommunication with manifold f. The gas passes upwardly through vessels31 of the first activation group and through the silica gel beds thereininto the tops thereof. As the hot gas passes through the adsorbentmaterial it removes the adsorbed moisture vapor and hydrocarbonstherefrom. From the tops of the vessels 31, the hot moisture,hydrocarbon laden-gas passes through flexible pipes 38 and openings 74in the upper tube sheet disc valve 35 into the upper manifold f. Fromthe upper manifold f," the hot gas passes through inlet-outlet conduit45 and pipe line 9 to the condenser separator 4 where the moisture andcondensable hydrocarbons are condensed and separated. The water andhydrocarbons are drained from the separator by a suitable drain line.From the condenser separator 4, the stripped captive gas passes throughpipe line 10 to the blower 3 and is recycled by the blower through pipeline 11, the heater 2 and pipe line 8 back through the first activationstage. This recirculation process is continuous.

The captive stream of gas in the first activation cycle is circulated bymeans of the blower 3, through the heater 2, the activation stage of theadsorber, and the condenser separator 4. The composition of this streamwill build up gradually in terms of condensable vapors, composed chieflyof hydrocarbons, until the dew point of the captive gas stream reachescondenser temperature, and will thereafter yield as liquid all thecondensable vapors desorbed in the activation stage of the adsorber.

In order to effect the complete removal of the desired hydrocarbons, asecond activation cycle following the first activation cycle isprovided. The activation gas, a captive gas, is heated in the heater 2,where its temperature is raised to about 500 F. From the heater, theheated activation gas passes through pipe line 12 and inlet-outletconduit 43' into the lower manifold d of the lower distributiveassemblage. From the manifold d the hot activation gas passes throughopenings 74 in the lower tube sheet disc valve 35 and flexible pipes 39into the lower end portions of the group of vessels 31 which are at thattime in communication with manifold d. The gas passes upwardly throughvessels 31 of the second activation group and through the silica gelbeds therein into the tops thereof. As the hot gas passes through theadsorbent material it removes all remaining hydrocarbons therefrom. Fromthe tops of the vessels 31, the hot hydrocarbon laden gas passes throughflexible pipes 38,

and openings 74 in the upper tube sheet disc valve 35 into the uppermanifold d. From the upper manifold d,".

the 'hot gas passes through inlet-outlet conduit 43 and pipe line 13 tothe blower 3', and is recycled by the blower through pipe line 14,heater 2, and pipe line 12, back through the second activation stage.This recycling process is continuous. t

In order to prevent dilution of the recycling activation gases and toprevent any loss of hydrocarbons into the effluent stripped gas from thelast adsorption stage, three purging stages are employed, a firstpurging stage immediately preceding the first activation stage, a secondpurging stage interposed between the first and second activation stages,and a third purging stage immediately following the third activationstage.

A portion of the recycling activation gas, used in the first activationstage, flowing through pipe line 11, is continuously diverted for use asthe purging medium in the first purging stage and passes through pipeline 15 and inlet-outlet conduit 46 into the lower manifold g of thelower distributive assemblage. From the manifeld g the purging gaspasses through openings 74 in the lower tube sheet disc valve 35 andflexible pipes 39 into the lower portions of the group of vessels 31which are at that time in communication with manifold g. The gas passesupwardly through the vessels 31 of the first purging stage and throughthe silica gel beds thereininto the tops thereof. As the purging gaspasses through the adsorbent material it removes the slippage naturalgas, thereby purging the beds. From the tops of the vessels 31 theeffluent gas, consisting substantially of slippage gas from the firstadsorption stage, passes through flexible pipes 38 and openings 74 inthe upper tube sheet disc valve 35 into the upper manifold g." From theupper manifold g the gas passes through inlet-outlet conduit 46 and pipethe adsorber.

A portion of the recycling activation gas used in the second activationstage flowing through pipe line 14 is continuously diverted for use asthe purging medium in the second purging stage and passes through pipeline 16 and inlet-outlet conduit 44 into the upper manifold e of theupper distributive assemblage. From the manifold e the purging gaspasses through openings 74 in the upper tube sheet disc valve 35 andflexible pipes 38 into the upper end portions of the group of vessels 31which are at that time in communication with manifold e. The gas passesdownwardly through the vessels 31 of the second purging stage andthrough the silica gel beds therein into the bottoms thereof. As thepurging gas passes through the adsorbent material it removes theslippage activation gas from the first activation stage; thereby purgingthe beds. From the bottoms of the vessels 31, the effluent gas,consisting substantially of slippage activation gas, passes throughflexible pipes 39 and openings 74 in the lower tube sheet disc valve 35"into the lower manifold e. From the lower manifold fe the gas passesthrough inlet-outlet conduit 44' and pipe line 17 to pipe line 10 andjoins the recycling activation gas used in the first activation stage.

The gas used as the purging gas in the third purging stage is obtainedby continuously diverting a portion of the flow of the stripped naturalgas through pipe line 7 from the last adsorption stage of the adsorber,through pipe line 18 and inlet-outlet conduit 42 into the upper manifoldc of the upper distributive assemblage. From the manifold c the purginggas passes through openings 74 in the upper tube sheet disc valve 35 andflexible pipes 38 into the upper end portions of the group of vessels 31which are at that time in communication with manifold c. The gas passesdownwardly through the vessels 31 and through the silica gel bedstherein into the bottoms thereof. As the purging gas passes through imaterial it removes the slippage activation j the adsorbent gas from thesecond activation stage, thereby purging line 15 into pipe line 5 andjoins the natural gas being treated on its way to the beds. From thebottoms of the vessels 31, the efliuent gas, consisting substantially ofslippage activation gas, passes through flexible pipe39 and openings 74into the lower tube sheet disc valve 35 into the lower manifold c. Fromthe lower manifold c the gas passes through inlet-outlet conduit 42 andpipe line 19 to pipe line 13 and joins the recycling activation gas usedin the second activation stage.

The gas being treated makes two passes through the adsorber, while eachof the activation gases and each of the purging gases each make a singlepass through the adsorber. For convenience in description, the stage ofthe adsorberthrough which the first adsorption passage of the gas beingtreated is made, is called the first adsorption stage, the stage throughwhich the second adsorption passage is made is called the secondadsorption stage, the stage through which the first activation gaspasses is called the first activation stage, the stage through which thesecond activation gas passes is called the second activation stage, thestage through which the first purging gas passes is called the firstpurging stage, the stage through which the second purging gas passes iscalled the second purging stage, and the stage through which the thirdpurging gas passes is called the third purging stage. Also, the vessels31 are called zones in which either adsorption, activation, or purgingtakes place, depending upon the particular fluid flowing therethrough ata given time. In addition, the condenser separator is called acondensing and separating zone or stage.

In the particular embodiment of the invention illustrated, the valvediscs 35 and the vessels 31 are rotated clockwise, as viewed in Fig. 2,and at a rate such that the efhuent gas flow from the purging stageswill be substantially volumetric with the slippage gas brought intothese stages as the vessels 31 are rotated; thus it will be seen that,as the valves 35 and the vessel 31 rotate, each of the vessels 31 willbe successively brought into communication with the manifolds g, f, e,d, c, b and a in the upper and lower distributive assemblages, so thateach vessel 31 will, in turn, become a first purging zone, a firstactivation zone, a second purging zone, a second activation zone, athird purging zone, a second adsorption zone, and a first adsorptionzone.

Suitable stop valves are provided at any desired point in any pipe lineto provide means for controlling the flow of the various mediums throughthe various stages of the adsorber and the auxiliary apparatus.

From the foregoing, it readily will be seen that there has been provideda novel and improved cyclic adsorption process for removing andrecovering moisture and condensable hydrocarbons from wet natural gas inwhich two activation steps are employed to effect a more completeremoval of the water vapor and desired hydrocarbons and a plurality ofpurging steps are employed so as to permit a build up of desorbedproducts in the recycling captive activation gas streams by preventingthe dilution of the activation gases by slippage gas and also to preventloss of desorbed products by slippage of activation gas into theoutgoing eflluent stripped natural gas.

While some of the flows of fluid through the apparatus have beendescribed as entering the top distributive assemblage and flowingdownward to and out of the bottom distributive assemblage, obviously,the flows may be in either direction.

Obviously, too, the present invention is not restricted to theparticular embodiments thereof herein shown and described.

What is claimed is:

1. In the process of treating wet natural gas to remove and/or recoverwater vapor and condensable hydrocarbons therefrom involving the contactof adsorbent matreial with the gas to be treated with resultantadsorption of the water vapor and condensable hydrocarbons by theadsorbent material and the subsequent treatment of the adsorbentmaterial with a heated medium to vaporize and 14 remove the water andcondensable hydrocarbons and thereby reactivate the adsorbent materialfor. further contact with the gas to be treated, the improvement whichcomprises rotating a series of separated beds of adsorbent materialdirectly in succession and substantially continuously relative to andthrough a first purging stage, a first activation stage, a secondpurging stage, a second activation stage, a third purging stage and atleast one adsorption stage; continuously directing a flow of the gasbeing treated, under high pressure and in succession, through theadsorption stages so that the water vapor and condensable hydrocarboncontent thereof which is to be removed will be adsorbed by the adsorbentmaterial there= in; continuously heating and recycling a flow of activation medium through said first activation stage to def sorb the waterand condensable hydrocarbons contained in the beds of adsorbent materialtherein and reactivate the adsorbent material; continuously heating andre cycling a flow of activation medium through said second activationstage to desorb the water and condensable hydrocarbons contained in thebeds of adsorbent material therein and reactivate the adsorbentmaterial; continuously diverting a portion of the flow ofthe recyclingactivation medium used in the first activation stage and directing itsflow through the first purging stage to remove all of the gas beingtreated therefrom; continuously directing the flow of the eflluent gasfrom the first purging stage into the flow of the gas being treated onits way to the first adsorption stage of the adsorber; continuouslydiverting a portion of the how of the recycling activation medium usedin the second activation stage and directing its flow through the secondpurging stage to remove all of the activation medium therefrom;continuously directing the flow of the effluent gas from the secondpurging stage into the flow of the recycling activation medium used inthe first activation stage; continuously diverting a portion of the flowof the efiiuent stripped gas being treated from the last of theadsorption stages and directing its flow through the third purgingstage: to remove all of the activation medium therefrom; continuouslydirecting the flow of the eflluent gas from the third purging stage intothe flow of the recycling activation medium used in the secondactivation stage; and continuously directing the flow of the captiveactivation medium used in the first activation stage as it is recycledand after its passage through the first activation stage, through acondensing and separating stage and there condensing and removing thewater and condensable hydrocarbons therefrom.

2. The process as set forth in claim 1, wherein the activation mediumrecycled through the first activation stage is heated to about 400 F.and the activation medium recycled through the second activation stageis heated to about 500 F.

3. In the process of treating wet natural gas to remove and/or recoverwater vapor and condensable hydrocarbons therefrom involving the contactof adsorbent material with the gas to be treated with resultantadsorption of the water vapor and condensable hydrocarbons by theadsorbent material and the subsequent treatment of the adsorbentmaterial with a heated medium to vaporize and remove the water andcondensable hydrocarbons and thereby reactivate the adsorbent materialfor further contact with the gas to be treated, the improvement whichcomprises maintaining at least one bed of adsorbent material in each ofa plurality of zones; continuously heating and recycling a first flow ofa captive activation medium through at least one of said zones to desorbthe water and condensable hydrocarbons contained in the beds ofadsorbent material therein and reactivate the adsorbent material;continuously heating and recycling a second how of a captive activationmedium through at least another one of said zones to desorb the waterand condensable hydrocarbons contained in the beds of adsorbent materialtherein and reactivate the adsorbent material, continuously directing afirst flow of a purging medium through at least another one of saidzones to purge the zone; continuously directing a second flow of apurging medium through at least another one of said zones to purge thezone; continuously directing a third flow of a purging medium through atleast another one of said zones to purge the zone; continuouslydirecting the flow of the gas being treated through the remainder ofsaid zones so that the water vapor and some of the condensablehydrocarbon content of the gas will be adsorbed by the adsorbentmaterial therein; periodically shifting the relative positions of theparticular adsorbent material and the particular flow of fluid in eachof said zones so that each zone becomes in succession a first purgingzone; a first activation zone, a second purging zone; a secondactivation zone, a third purging zone and an adsorption zone;continuously diverting a portion of said first flow of a captiverecycling activation medium for use as the first purging medium andcontinuously directing the flow of the efiluent gas from the firstpurging zone back into the flow of the gas being treated on its way tothe first adsorption zone; continuously diverting a portion of saidsecond flow of a captive recycling activation medium for use as thesecond purging medium and continuously directing the flow of theefiluent gas from the second purging zone into said first flow of acaptive recycling activation medium; continuously diverting a portion ofthe flow of stripped efil'uent gas from the last adsorption zone for useas the third purging medium and continuously directing the flow of theeffiuent gas from the third purging zone into said second flow of acaptive recycling activation medium; and continuously directing saidfirst flow of a captive recycling activation medium as it is recycledand after its passage through the first activation zone, through acondensing and separating zone and there condensing and removing theWater and condensable hydrocarbons therefrom.

4. The process as set forth in claim 3, wherein the activation mediumrecycled through the first activation zone is heated to about 400 F. andthe activation medium recycled through the second activation zone isheated to about 500 F.

References Cited in the file of this patent UNITED STATES PATENTS1,721,033 Okochi July 16, 1929 1,998,774 Bulkeley Apr. 23, 19352,739,669 Miller Mar. 27, 1956 2,739,670 Miller Mar. 27, 1956 2,771,964Miller Nov. 27, 1956

1. IN THE PROCESS OF TREATING WET NATURAL GAS TO REMOVE AND/OR RECOVERWATER VAPOR AND CONDENSATE HYDROCARBONS THEREFROM INVOLVING THE CONTACTOF ADSORBENT MATERIAL WITH THE GAS TO BE TREATED WITH RESULTANTADSORPTION OF THE WATER VAPOR AND CONDENSABLE HYDROCARBONS BY THEADSORBENT MATERIALS AND SUBSEQUENT TREATMENT OF THE ADSORBENT MATERIALWITH A HEATED MEDIUM TO VAPORIZE AND REMOVE THE WATER AND CONDENSABLEHYDROCARBONS AND THEREBY REACTIVATE THE ADSORBENT MATERIAL FOR FURTHERCONTACT WITH THE GAS TO BE TREATED, THE IMPROVEMENT WHICH COMPRISESROTATING A SERIES OF SEPARATED BEDS OF ADSORBENT MATERIAL DIRECTLY INSUCCESSION AND SUBSTANTIALLY CONTINUOUSLY RELATIVE TO AND THROUGH AFIRST PURGING STAGE, A FIRST ACTIVATION STAGE, A SECOND PURGING STAGE, ASECOND ACTIVE TION STAGE, A THIRD PURGING STAGE AND AT LEAST ONEADSORBTION STAGE, CONTINUOUSLY DIRECTING A FLOW OF THE GAS BEINGTREATED, UNDER HIGH PRESSURE AND IN SUCCESSION, THROUGH THE ADSORPTIONSTAGES SO THAT THE WATER VAPOR AND CONDENSABLE HYDROCARBON CONTENTTHEREOF WHICH IS TO BE REMOVED WILL BE ADSORBED BY THE ADSORBENTMATERIAL THEREIN, CONTINUOUSLY HEATING AND RECYCLING A FLOW OFACTIVATION MEDIUM THROUGH SAID FIRST ACTIVATION STAGE TO DESORB THEWATER AND CONDENSABLE HYDROCARBONS CONTAINED IN THE BEDS OF ADSORBENTMATERIAL THEREIN AND REACTIVATE THE ADSORBENT MATERIAL; CONTINUOUSLYHEATING AND RECYCLING A FLOW OF ACTIVATION MEDIUM THROUGH SAID SECONDACTIVATION STAGE TO DESORB THE WATER AND CONDENSABLE HYDROCARBONSCONTAINED IN THE BEDS OF ADSORBENT MATERIAL THEREIN AND THE ADSORBENTMATERIAL; CONTINUOUSLY DIVERTING A PORTION OF THE FLOW OF THE RECYCLINGACTIVATION MEDIUM USED IN THE FIRST ACTIVATION STAGE AND DIRECTING ITSFLOW THROUGH THE FIRST PURGING STAGE TO REMOVE ALL OF THE GAS BEINGTREATED THEREFROM, CONTINUOUSLY DIRECTING THE FLOW OF THE EFFLUENT GASFROM THE FIRST PURGING STAGE INTO THE FLOW OF THE GAS BEING TREATED ONITS WAY TO THE FIRST ADSORPTION STAGE OF THE ADSORBER, CONTINUOUSLYDIVERTING A PORTION OF THE FLOW OF THE RECYCLING ACTIVATION MEDIUM USEDIN THE SECOND ACTIVATION STAGE AND DIRECTING ITS FLOW THROUGH THE SECONDPURGING STAGE TO REMOVE ALL OF THE ACTIVATION MEDIUM THEREFROM,CONTINUOUSLY DIRECTING THE FLOW OF THE EFFLUENT GAS FROM THE SECONDPURGING STAGE INTO THE FLOW OF THE RECYCLING ACTIVATION MEDIUM USED INTHE FIRST ACTIVATION STAGE, CONTINUOUSLY DIVERTING A PORTION OF THE FLOWOF THE EFFLUENT STRIPPED GAS BEING TREATED FROM THE LAST OF THEADSORPTION STAGES AND DIRECTING ITS FLOW THROUGH THE THIRD PURGING STAGETO REMOVE ALL OF THE ACTIVATION MEDIUM THEREFROM, CONTINUOUSLY DIRECTINGTHE FLOW OF THE EFFLUENT GAS FROM THE THIRD PURGING STAGE INTO THE FLOWOF THE RECYCLING ACTIVATION MEDIUM USED IN THE SECOND ACTIVATION STAGE,AND CONTINUOUSLY DIRECTING THE FLOW OF THE CAPTIVE ACTIVATION MEDIUMUSED IN THE FIRST ACTIVATION STAGE AS IT IS RECYCLED AND AFTER ITSPASSAGE THROUGH THE FIRST ACTIVATION STAGE, THROUGH A CONDENSING ANDSEPARATING STAGE AND THERE CONDENSING AND REMOVING THE WATER ANDCONDENSATE HYDROCARBONS THEREFROM.